JPH06319964A - Flat membrane type filter - Google Patents
Flat membrane type filterInfo
- Publication number
- JPH06319964A JPH06319964A JP13691793A JP13691793A JPH06319964A JP H06319964 A JPH06319964 A JP H06319964A JP 13691793 A JP13691793 A JP 13691793A JP 13691793 A JP13691793 A JP 13691793A JP H06319964 A JPH06319964 A JP H06319964A
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- JP
- Japan
- Prior art keywords
- membrane
- flat
- filtration
- plate
- amplitude
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、懸濁質を含んだ原水の
処理に使用する平膜型濾過装置に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a flat sheet membrane type filtration device used for treating raw water containing suspended solids.
【０００２】[0002]
【従来の技術】懸濁質を含有する原水、例えば、河川水
を浄化処理する装置として、開放型の被処理液槽内に、
平型濾過膜セルを複数箇相互に間隔を隔てて立設し、平
型濾過膜セル内を真空ポンプにより減圧して濾過に必要
な膜間差圧を発生させ、原液供給量を濾過液流量と平衡
させつつ原液を供給して原液を処理する平膜型濾過装置
が公知である。2. Description of the Related Art As an apparatus for purifying raw water containing suspended matter, for example, river water, an open type liquid tank to be treated,
A plurality of flat filtration membrane cells are erected at intervals from each other, and the pressure inside the flat filtration membrane cell is reduced by a vacuum pump to generate the transmembrane pressure difference necessary for filtration, and the raw liquid supply rate is the filtrate flow rate. There is known a flat sheet membrane-type filtration device for treating the stock solution by supplying the stock solution while being balanced.
【０００３】周知の通り、平膜型濾過装置においては、
膜面への固形分の付着による経時的な濾過流量の低下が
避けられず、特に、上記した高濃度懸濁液の場合、その
濾過流量の低下が顕著であって、相当頻繁な膜洗浄が必
要である。As is well known, in the flat sheet membrane filtration device,
It is inevitable that the filtration flow rate will decrease over time due to the adherence of solids to the membrane surface. In particular, in the case of the above-mentioned high-concentration suspension, the reduction in the filtration flow rate is remarkable, and a fairly frequent membrane cleaning is required. is necessary.
【０００４】従来、中空糸膜モジュ−ルを対象とした膜
洗浄方法として、エア−スクラビング法、すなわち、原
液中にエア−を噴出させ、この噴出エア−と原液との混
合流で膜面付着物を剥離・除去する方法が知られてお
り、膜面への気液混合流の接触に加え、中空糸膜の揺動
による相互接触も付着物剥離を促す要因となっている。Conventionally, as a membrane cleaning method for hollow fiber membrane modules, an air-scrubbing method, that is, air is jetted into a stock solution and the membrane surface is attached by a mixed flow of the jetted air and the stock solution. A method for peeling and removing the kimono is known, and in addition to the contact of the gas-liquid mixed flow to the membrane surface, mutual contact due to rocking of the hollow fiber membrane is also a factor that promotes the peeling of the adhered matter.
【０００５】[0005]
【発明が解決しようとする課題】上記した平膜型濾過装
置の平型濾過膜セルにおいては、中空糸膜に較べて剛性
が高く、上記気液混合流による揺動が軽度であり、膜相
互の接触が少なく、上記のエア−スクラビング法を単に
適用しても、さしたる効果は期待できない。DISCLOSURE OF THE INVENTION In the flat filtration membrane cell of the flat membrane filtration apparatus described above, the rigidity is higher than that of the hollow fiber membrane, the fluctuation due to the gas-liquid mixed flow is mild, and the membrane mutual However, even if the above-mentioned air-scrubbing method is simply applied, no significant effect can be expected.
【０００６】上記平膜型濾過装置の膜洗浄方法として、
平型濾過膜セルの濾過側を減圧する真空ポンプに並列に
液送ポンプを接続し、真空ポンプを停止し液送ポンプを
駆動して濾過液を逆送する方法（特開昭５５−１１０６
１号公報）、作業者が被処理液槽外から平型濾過膜セル
間にブラシを挿入する方法等が公知であるが、前者にお
いては、平型濾過膜セルの膨張破裂の危険性があり、後
者においては、多大な労力と作業時間が余儀なくされ
る。[0006] As a membrane cleaning method for the flat membrane filtration device,
A method in which a liquid feed pump is connected in parallel to a vacuum pump for depressurizing the filtration side of a flat filtration membrane cell, and the vacuum pump is stopped and the liquid feed pump is driven to feed back the filtrate (JP-A-55-1106).
No. 1), a method is known in which an operator inserts a brush between the flat filtration membrane cells from outside the liquid tank to be treated, but in the former, there is a risk of expansion and rupture of the flat filtration membrane cells. In the latter case, a great deal of labor and working time are forced.
【０００７】本発明の目的は、エア−スクラビング法に
よって膜洗浄を効率よく行うことのできる平膜型濾過装
置を提供することにある。An object of the present invention is to provide a flat sheet membrane type filtration device which can efficiently perform membrane cleaning by the air-scrubbing method.
【０００８】[0008]
【課題を解決するための手段】本発明の平膜型濾過装置
は、膜の内側に濾過液流路を有する平型濾過膜セルを複
数枚、乱流発生板を介して積層し、該積層体を巾両端に
おいて結着し、上記セルと乱流発生板との間に原液流路
間隙を保持した膜ユニットを被処理液槽内に浸漬設置
し、同上膜ユニットの下方に散気配管を設けたことを特
徴とする構成であり、乱流発生板に波付き板を使用し、
波形のピッチｐと振幅ｈとの比ｐ／ｈを２〜１８とし、
膜面と波付き板との最小流路高さｂと振幅ｈとの比ｈ／
ｂを１．０〜３．０とすることが好ましい。In the flat sheet membrane filtration apparatus of the present invention, a plurality of flat sheet membrane cells having a filtrate flow path inside the membrane are laminated through a turbulent flow generation plate, and the laminated membranes are laminated. The body is bound at both ends of the width, and the membrane unit holding the undiluted solution flow path gap between the cell and the turbulent flow generation plate is dipped and installed in the liquid tank to be treated. It is a feature that is provided, using a corrugated plate for the turbulent flow generation plate,
The ratio p / h between the waveform pitch p and the amplitude h is set to 2 to 18,
Ratio h / of minimum flow path height b between membrane surface and corrugated plate and amplitude h
It is preferable that b is 1.0 to 3.0.
【０００９】[0009]
【作用】平型濾過膜セルと乱流発生板、例えば、波付き
板との間の原液流路間隙が波付き板のピッチで広狭に変
化し、膜洗浄時、この原液流路間隙に、下方の散気配管
からの放散エアと原液との混合流体が流れてその混合流
体の乱流化が促され、この乱流発生に伴い発生する振動
と乱流との相乗作用により、膜面付着物の剥離が効果的
に行われる。[Function] The stock solution flow path gap between the flat filtration membrane cell and the turbulent flow generation plate, for example, the corrugated plate changes widely with the pitch of the corrugated plate, and when the membrane is washed, the stock solution flow path gap is The mixed fluid of the diffused air and the undiluted solution flows from the diffuser pipe below, and the turbulence of the mixed fluid is promoted. The kimono is effectively peeled off.
【００１０】[0010]
【実施例】以下、図面により本発明の実施例を説明す
る。図１は本発明において使用する平型濾過膜セル１を
示し、濾過液流路保持部材（例えば、ポリエチレン等の
ポリオレフィン系、塩化ビニル等のネット、多孔プラス
チックシ−ト等）１１の両面に半透性平膜（ポリエステ
ル製またはポリエチレン製不織布上に膜素材、例えば、
ポリスルホン、ポリエ−テルスルホン、ポリアクリロニ
トリル、ポリエチレン、ポリプロピレン等の膜層を形成
したもの、膜層内にポリエステル製またはポリエチレン
製織布を埋め込んだものを使用できる）１２を添付し、
上下の縁端を接着剤１３で封止したものを使用できる
（寸法は、通常、横１０〜２００ｃｍ，縦３〜１５０ｃ
ｍ程度）。Embodiments of the present invention will be described below with reference to the drawings. FIG. 1 shows a flat-type filtration membrane cell 1 used in the present invention, in which both sides of a filtrate flow channel holding member (for example, polyolefin such as polyethylene, net such as vinyl chloride, porous plastic sheet, etc.) Transparent flat membrane (membrane material on polyester or polyethylene non-woven fabric, for example,
A film having a film layer formed of polysulfone, polyethersulfone, polyacrylonitrile, polyethylene, polypropylene or the like, or a film made of a polyester or polyethylene woven fabric embedded in the film layer can be used) 12 is attached,
It is possible to use one in which the upper and lower edges are sealed with an adhesive agent 13 (the dimensions are usually 10 to 200 cm in width and 3 to 150 c in length).
m).
【００１１】図２は本発明において使用する膜ユニット
Ａを示している。図２において、１は上記した平型濾過
膜セル、２は乱流発生板例えば、波付き板（ステンレス
板、FRP板等を使用できる）であり、これらを相互に積
層し、両側に波付き板２を配し、平型濾過膜セル１の膜
面と波付き板２との間に原液流路間隙３を保持してあ
る。FIG. 2 shows a membrane unit A used in the present invention. In FIG. 2, 1 is the above-mentioned flat filtration membrane cell, 2 is a turbulent flow generation plate, for example, a corrugated plate (stainless steel plate, FRP plate, etc. can be used), which are laminated on each other and corrugated on both sides. A plate 2 is arranged, and a stock solution flow passage gap 3 is held between the membrane surface of the flat filtration membrane cell 1 and the corrugated plate 2.
【００１２】４１は積層体の両端側に接着剤により固着
した枠縁、４２は枠縁４１内に樹脂の注入により形成し
た隔壁（エポキシ系、ウレタン系、シリコ−ン系等の硬
化性樹脂を使用できる）、４３はパッキング、４４は濾
過液取出し用キャップであり、キャップ４４内は外部か
ら、上記の隔壁４２とパッキング４３とにより水密に遮
断されている。Reference numeral 41 denotes a frame edge fixed to both ends of the laminate with an adhesive, and 42 denotes a partition wall formed by injecting resin into the frame edge 41 (curable resin such as epoxy type, urethane type, or silicone type curable resin). 43) is a packing, and 44 is a filtrate removing cap. The inside of the cap 44 is watertightly blocked from the outside by the partition wall 42 and the packing 43.
【００１３】上記平型濾過膜セルＡにおいては、エア−
スクラビング時、気液混合流体の原液流路間隙３への流
入により撓み変形するから、枠縁近傍部分（３〜１００
ｍｍ程度の長さ部分）を柔軟性材料で補強することが好
ましい。In the flat filtration membrane cell A, the air-
At the time of scrubbing, the gas-liquid mixed fluid is flexibly deformed by flowing into the raw liquid flow path gap 3, so that a portion (3 to 100) near the frame edge is deformed.
It is preferable that a portion having a length of about mm) is reinforced with a flexible material.
【００１４】図３は図２におけるIII−III断面図であ
り、ｐは波付き板２のピッチを、ｈは振幅を、ｂは膜面
１２と波付き板２との最小流路高さをそれぞれ示してい
る。この最小流路高さｂの確保のために、積層体の両端
部にスペ−サが介在されるが、図２において、このスペ
−サの図示は、省略してある。FIG. 3 is a sectional view taken along line III-III in FIG. 2, where p is the pitch of the corrugated plate 2, h is the amplitude, and b is the minimum flow path height between the membrane surface 12 and the corrugated plate 2. Shown respectively. Spacers are provided at both end portions of the laminated body in order to secure the minimum flow path height b, but the spacers are not shown in FIG.
【００１５】図４は本発明の平膜型濾過装置の実施例を
示す説明図である。図４において、５１は開放型の被処
理液槽である。５２は原液供給配管、５３は原液供給ポ
ンプである。Ａは被処理液槽５１内に浸漬配設した既述
の膜ユニットである。５４は濾過液取り出し配管、５５
は真空ポンプ、５６は流量計、５７は濾過液貯留槽であ
る。５８は膜ユニットＡの直下に配設した散気配管、５
９はブロワである。FIG. 4 is an explanatory view showing an embodiment of the flat sheet membrane filtration device of the present invention. In FIG. 4, 51 is an open type liquid tank to be treated. Reference numeral 52 is a stock solution supply pipe, and 53 is a stock solution supply pump. A is the above-mentioned membrane unit which is immersed in the liquid tank 51 to be treated. 54 is a filtrate take-out pipe, 55
Is a vacuum pump, 56 is a flow meter, and 57 is a filtrate storage tank. Reference numeral 58 is a diffuser pipe arranged immediately below the membrane unit A, 5
9 is a blower.
【００１６】この平膜型濾過装置により原液を処理する
には、原液供給ポンプ５３の駆動により被処理液槽５１
内に原液を供給し、真空ポンプ５５を駆動し膜ユニット
Ａの濾過側を減圧して、濾過に必要な膜間差圧を発生さ
せ、かかる膜間差圧のもとで濾過を進め、この濾過流量
にほぼ等しい流量で原液を連続的または間歇的に供給
し、被処理液槽５１内の原液水位をほほ一定に保持しつ
つ原液を処理していく。To process the stock solution with this flat sheet membrane filtration device, the stock solution supply pump 53 is driven to supply the solution tank 51 to be processed.
The undiluted solution is supplied to the inside, the vacuum pump 55 is driven, the filtration side of the membrane unit A is decompressed, and the transmembrane pressure required for filtration is generated. The stock solution is continuously or intermittently supplied at a flow rate substantially equal to the filtration flow rate, and the stock solution is processed while maintaining the water level of the stock solution in the liquid tank 51 to be treated almost constant.
【００１７】この原液処理と並行して、一定期間ごとに
一定時間、ブロワ５９を駆動し、散気配管５８からエア
を原液中に放散させ、エア−スクラビングを行う。この
場合、放散エアと原液との混合流体が上昇し、膜ユニッ
トＡの原液流路間隙３を通過し、この原液流路間隙３が
波付き板２のために広狭と変化し、これに伴い、気液混
合流体の上昇流速が変化するので、乱流が発生し、同時
にその流速変動に伴い乱流発生板である波付き板２に振
動が発生する。而るに、乱流発生板と平型濾過膜セルと
を巾両端において結着してあるので、乱流発生板の振動
が平型濾過膜セルの膜面によく伝達され、この膜面振動
と膜面での乱流との相乗作用により、膜面付着物の剥
離、除去が効果的に剥離され、良好な洗浄が保障され
る。In parallel with this undiluted solution treatment, the blower 59 is driven for a definite period of time for a definite period of time, air is diffused into the undiluted solution from the diffuser pipe 58, and air-scrubbing is performed. In this case, the mixed fluid of the diffused air and the stock solution rises and passes through the stock solution flow path gap 3 of the membrane unit A, and the stock solution flow path gap 3 changes widely due to the corrugated plate 2. Since the rising flow velocity of the gas-liquid mixed fluid changes, turbulent flow occurs, and at the same time, the corrugated plate 2 serving as the turbulent flow generating plate also vibrates due to the change in the flow velocity. Thus, since the turbulent flow generating plate and the flat filtration membrane cell are connected at both ends of the width, the vibration of the turbulent flow generating plate is well transmitted to the membrane surface of the flat filtration membrane cell, and this membrane surface vibration By the synergistic effect of the turbulent flow on the film surface, the film surface deposits are effectively separated and removed, and good cleaning is ensured.
【００１８】上記エア−スクラビングのエア−流量は、
高くし過ぎると膜の物理的強度の低下が惹起されるの
で、膜面積１m2当たり、０．１〜３Nm3/h好ましくは、
０．２〜２Nm3/hとされる。The air flow rate of the air scrubbing is
If it is made too high, the physical strength of the film will be lowered, so 0.1 to 3 Nm 3 / h per 1 m 2 of the film area is preferable.
It is set to 0.2 to 2 Nm 3 / h.
【００１９】上記波付き板２において、ピッチｐと振幅
ｈとの比ｐ／ｈを余り小さくすると、蛇行形状が深くな
り、谷の部分でのエア−溜り、懸濁物質の蓄積が生じ易
くなると共に、単位長さ当たりの波数が多くなって乱流
効果の低下が懸念される。一方、比ｐ／ｈを余り大きく
すると、乱流効果の低下が懸念される。In the corrugated plate 2, if the ratio p / h of the pitch p and the amplitude h is made too small, the meandering shape becomes deep, and air accumulation in the valley portion and accumulation of suspended substances easily occur. At the same time, there is concern that the number of waves per unit length increases and the turbulent flow effect decreases. On the other hand, if the ratio p / h is made too large, there is a concern that the turbulence effect may be reduced.
【００２０】また、膜面と波付き板との最小流路高さｂ
と振幅ｈとの比ｈ／ｂを余り大きくすると、気液混合流
体通路の確保が困難になると共にエア−溜りが発生し易
くなる。一方、比ｈ／ｂを余り小さくすると、気液混合
流体通路が直線状となり、乱流効果の低下が懸念され
る。Also, the minimum flow path height b between the film surface and the corrugated plate
If the ratio h / b between the amplitude h and the amplitude h is made too large, it becomes difficult to secure the gas-liquid mixed fluid passage and air-pumps easily occur. On the other hand, if the ratio h / b is made too small, the gas-liquid mixed fluid passage becomes linear, and there is a concern that the turbulence effect may be reduced.
【００２１】従って、波形のピッチｐと振幅ｈとの比ｐ
／ｈは２〜１８とし、膜面と波付き板との最小流路高さ
ｂと振幅ｈとの比ｈ／ｂは１．０〜３．０とすることが
好ましい。Therefore, the ratio p between the waveform pitch p and the amplitude h
/ H is 2 to 18, and the ratio h / b of the minimum flow path height b between the film surface and the corrugated plate and the amplitude h is preferably 1.0 to 3.0.
【００２２】上記乱流発生板は、波付き板のみに限定さ
れるものではない。例えば、図５の（イ）並びに図５の
（ロ）〔図５の（イ）のロ−ロ断面図〕に示すように、
平板２１の両面または片面に波形の凸条２２を成形した
プラスチック板を使用することもできる。The turbulent flow generation plate is not limited to the corrugated plate. For example, as shown in (a) of FIG. 5 and (b) of FIG. 5 [a cross-sectional view of (a) of FIG. 5],
It is also possible to use a plastic plate having corrugated ridges 22 formed on both sides or one side of the flat plate 21.
【００２３】本発明の平膜型濾過装置においては、経時
的な濾過流量の低下をよく抑制でき、濾過流量を高く保
持することができる。このことは次の実施例と比較例と
の対比からも明らかである。In the flat sheet membrane filtration apparatus of the present invention, it is possible to well suppress the decrease of the filtration flow rate with time, and to keep the filtration flow rate high. This is clear from the comparison between the following examples and comparative examples.
【００２４】実施例１ 図１に示す平型濾過膜セル１には、濾過流路保持部材１
１が厚さ０．１２mmのポリプロピレン製ネット、平膜１
２が分画分子量７５万のポリスルホン膜、寸法が横１２
０cm，縦６０cmであるものを使用した。波付き板２に
は、波形のピッチｐと振幅ｈとの比ｐ／ｈが３．０，厚
さがmmのステンレ板を使用した。平膜型濾過装置の積層
体においては、上記平型濾過膜セル６枚と波付き板とを
積層し（両側は波付き板）、図３における膜面と波付き
板との最小流路高さｂを４mmとし、最小流路高さｂと振
幅ｈとの比ｈ／ｂを１．０とした。平膜型濾過装置の有
効膜面積は約６m2であった。Example 1 In the flat filtration membrane cell 1 shown in FIG.
1 is a 0.12 mm thick polypropylene net, flat membrane 1
2 is a polysulfone membrane with a cut-off molecular weight of 750,000, the dimensions are 12 horizontal
The one having a length of 0 cm and a length of 60 cm was used. As the corrugated plate 2, a stainless plate having a ratio p / h of the waveform pitch p to the amplitude h of 3.0 and a thickness of mm was used. In the laminated body of the flat membrane type filtration device, the above-mentioned 6 pieces of flat type membrane filter cells and the corrugated plate are laminated (the corrugated plates on both sides), and the minimum flow path height between the membrane surface and the corrugated plate in FIG. The height b was 4 mm, and the ratio h / b between the minimum flow path height b and the amplitude h was 1.0. The effective membrane area of the flat sheet membrane filter was about 6 m 2 .
【００２５】この実施例装置を使用して、エア−スクラ
ビングを、膜面積１m2当たりエア−流量２Nm3/h、３０
分ごとに１分間行いながら、濁度１０の河川水を濾過処
理したところ、濾過流速は図６の曲線Ｉの通りであり、
連続運転１ヵ月後の濾過流速は０．８５m3/(m2・day)で
あった。Using the apparatus of this example, air-scrubbing was performed at an air flow rate of 2 Nm 3 / h, 30 per 1 m 2 of membrane area.
When the river water having a turbidity of 10 was subjected to a filtration treatment while being carried out for 1 minute every minute, the filtration flow rate was as shown by the curve I in FIG.
The filtration flow rate after one month of continuous operation was 0.85 m 3 / (m 2 · day).
【００２６】比較例 波付き板を使用せず、平型濾過膜セル間の間隔を４mmと
した以外、実施例と同じとした。実施例と同様にして運
転したところ、濾過流速は図６の曲線IIの通りであり、
連続運転１ヵ月後の濾過流速は０．６７５m3/(m2・day)
であった。Comparative Example The same as Example except that the corrugated plate was not used and the distance between the flat filtration membrane cells was 4 mm. When operated in the same manner as in the example, the filtration flow rate is as shown by the curve II in FIG.
The filtration flow rate after one month of continuous operation is 0.675 m 3 / (m 2 · day)
Met.
【００２７】図６の曲線ＩとIIとの比較から、本発明の
平膜型濾過装置においては、従来装置に較べ、高い濾過
流速を保障できることが明らかである。なお、実施例１
に対し、ｈ／ｂを０．５（ｈ＝４mm)とし、他の条件は
実施例に同じとした場合の連続運転１ヵ月後の濾過流速
は０．７００m3/(m2・day)であり、実施例１に対し、ｐ
／ｈを２５（ｈ＝４mm)とし、他の条件は実施例に同じ
とした場合の連続運転１ヵ月後の濾過流速は０．７１０
m3/(m2・day)であり、実施例１に対し、ｐ／ｈを１（ｈ
＝４mm)とし、他の条件は実施例に同じとした場合の連
続運転１ヵ月後の濾過流速は０．７７０m3/(m2・day)で
あり、何れの場合も、比較例に較べ、高い濾過流速であ
った。From the comparison between the curves I and II in FIG. 6, it is clear that the flat sheet membrane filtration device of the present invention can guarantee a higher filtration flow rate than the conventional device. In addition, Example 1
On the other hand, when h / b was 0.5 (h = 4 mm) and the other conditions were the same as in the example, the filtration flow rate after one month of continuous operation was 0.700 m 3 / (m 2 · day). Yes, in contrast to Example 1, p
/ H is set to 25 (h = 4 mm) and the other conditions are the same as in the example, the filtration flow rate after one month of continuous operation is 0.710.
m 3 / (m 2 · day), and p / h is 1 (h
= 4 mm) and the other conditions were the same as in the example, the filtration flow rate after one month of continuous operation was 0.770 m 3 / (m 2 · day), and in each case, compared with the comparative example, High filtration flow rate.
【００２８】[0028]
【発明の効果】本発明の平膜型濾過装置は、上述した通
りの構成であり、平型濾過膜セルと乱流発生板との積層
化によって、エア−スクラビング時、放散エアと原液と
の混合流体の膜面での乱流化を促し、かつ乱流時に発生
する振動を膜面に伝達させるようにしているから、その
乱流と振動との相乗作用により、効果的な膜面洗浄を保
障でき、高濾過流速の平膜型濾過装置を提供できる。EFFECT OF THE INVENTION The flat sheet membrane filtration device of the present invention is constructed as described above, and the flat sheet membrane membrane cell and the turbulent flow generation plate are laminated, whereby air-scrubbing is carried out so that the diffused air and the stock solution are separated. Since the turbulent flow of the mixed fluid is promoted on the film surface and the vibration generated during the turbulent flow is transmitted to the film surface, the synergistic effect of the turbulent flow and vibration enables effective film surface cleaning. It is possible to provide a flat membrane type filtration device which can be guaranteed and has a high filtration flow rate.
【図１】本発明において使用される平型濾過膜セルを示
す説明図である。FIG. 1 is an explanatory view showing a flat filtration membrane cell used in the present invention.
【図２】本発明において使用される膜ユニットを示す説
明図である。FIG. 2 is an explanatory view showing a membrane unit used in the present invention.
【図３】図２におけるIII−III断面説明図である。3 is a cross-sectional view taken along the line III-III in FIG.
【図４】本発明の実施例を示す説明図である。FIG. 4 is an explanatory diagram showing an example of the present invention.
【図５】図５の（イ）は本発明において使用する乱流発
生板の別例を示す説明図、図５の（ロ）は図５の（イ）
におけるロ−ロ断面説明図である。5 (a) is an explanatory view showing another example of the turbulent flow generation plate used in the present invention, and FIG. 5 (b) is FIG. 5 (a).
FIG. 4 is a cross-sectional explanatory view taken along line ‘
【図６】本発明の実施例と比較例との濾過流速特性を示
す図表である。FIG. 6 is a chart showing filtration flow rate characteristics of an example of the present invention and a comparative example.
１ 平型濾過膜セル １２ 膜 ２ 乱流発生板 ３ 原液流路間隙 Ａ 膜ユニット ５１ 被処理液槽 ５８ 散気配管 ５９ ブロワ 1 Flat Type Filtration Membrane Cell 12 Membrane 2 Turbulent Flow Generation Plate 3 Raw Liquid Flow Path Gap A Membrane Unit 51 Treatment Liquid Tank 58 Diffusing Pipe 59 Blower
Claims (2)
セルを複数枚、乱流発生板を介して積層し、該積層体を
巾両端において結着し、上記セルと乱流発生板との間に
原液流路間隙を保持した膜ユニットを被処理液槽内に浸
漬設置し、同上膜ユニットの下方に散気配管を設けたこ
とを特徴とする平膜型濾過装置。1. A plurality of flat filtration membrane cells each having a filtrate flow channel inside the membrane are laminated via a turbulent flow generation plate, and the laminated body is bound at both ends of the width to form a turbulent flow with the cell. A flat sheet membrane type filtration device characterized in that a membrane unit having a raw liquid flow path gap held between it and a generating plate is dipped and installed in a liquid tank to be treated, and an air diffusion pipe is provided below the membrane unit.
ッチｐと振幅ｈとの比ｐ／ｈを２〜１８とし、膜面と波
付き板との最小流路高さｂと振幅ｈとの比ｈ／ｂを１．
０〜３．０とした請求項１記載の平膜型濾過装置。2. A corrugated plate is used as the turbulent flow generating plate, the ratio p / h of the waveform pitch p and the amplitude h is set to 2 to 18, and the minimum flow path height b between the membrane surface and the corrugated plate is set. The ratio h / b between the amplitude and the amplitude h is 1.
The flat sheet membrane-type filtration device according to claim 1, wherein the filtration device has a thickness of 0 to 3.0.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13691793A JPH06319964A (en) | 1993-05-15 | 1993-05-15 | Flat membrane type filter |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13691793A JPH06319964A (en) | 1993-05-15 | 1993-05-15 | Flat membrane type filter |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH06319964A true JPH06319964A (en) | 1994-11-22 |
Family
ID=15186600
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP13691793A Pending JPH06319964A (en) | 1993-05-15 | 1993-05-15 | Flat membrane type filter |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH06319964A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003086987A1 (en) * | 2002-04-12 | 2003-10-23 | Seghers Keppel Technology Group | Method and device for purifying a liquid medium |
| JP2005058818A (en) * | 2003-08-12 | 2005-03-10 | Ando Seisakusho:Kk | Filter block and water purification apparatus equipped with the same |
| KR100722332B1 (en) * | 2006-11-06 | 2007-05-28 | 주식회사 퓨어엔비텍 | A block type membrane module frame |
| JP2008173556A (en) * | 2007-01-17 | 2008-07-31 | Hitachi Ltd | Sewage treatment apparatus |
| KR101007878B1 (en) * | 2010-07-09 | 2011-01-14 | 이코리더 주식회사 | Block type membrane module |
| WO2013103083A1 (en) * | 2012-01-05 | 2013-07-11 | 住友重機械工業株式会社 | Membrane separation method and membrane separation apparatus |
| KR101467253B1 (en) * | 2012-09-14 | 2014-12-01 | 주식회사 부강테크 | Membrane filter having fixed vortex-inducing layers |
-
1993
- 1993-05-15 JP JP13691793A patent/JPH06319964A/en active Pending
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003086987A1 (en) * | 2002-04-12 | 2003-10-23 | Seghers Keppel Technology Group | Method and device for purifying a liquid medium |
| JP2005058818A (en) * | 2003-08-12 | 2005-03-10 | Ando Seisakusho:Kk | Filter block and water purification apparatus equipped with the same |
| JP4722185B2 (en) * | 2006-11-06 | 2011-07-13 | ピュア−エンビテック カンパニー リミテッド | Block type flat membrane module frame |
| KR100722332B1 (en) * | 2006-11-06 | 2007-05-28 | 주식회사 퓨어엔비텍 | A block type membrane module frame |
| WO2008056863A1 (en) * | 2006-11-06 | 2008-05-15 | Pure-Envitech Co., Ltd. | Block type membrane module frame |
| JP2009509766A (en) * | 2006-11-06 | 2009-03-12 | ピュア−エンビテック カンパニー リミテッド | Block type flat membrane module frame |
| JP2008173556A (en) * | 2007-01-17 | 2008-07-31 | Hitachi Ltd | Sewage treatment apparatus |
| KR101007878B1 (en) * | 2010-07-09 | 2011-01-14 | 이코리더 주식회사 | Block type membrane module |
| WO2012005448A2 (en) * | 2010-07-09 | 2012-01-12 | 이코리더 주식회사 | Block type flat membrane module |
| WO2012005448A3 (en) * | 2010-07-09 | 2012-05-03 | 이코리더 주식회사 | Block type flat membrane module |
| WO2013103083A1 (en) * | 2012-01-05 | 2013-07-11 | 住友重機械工業株式会社 | Membrane separation method and membrane separation apparatus |
| CN104010716A (en) * | 2012-01-05 | 2014-08-27 | 住友重机械工业株式会社 | Membrane separation method and membrane separation apparatus |
| JPWO2013103083A1 (en) * | 2012-01-05 | 2015-05-11 | 住友重機械工業株式会社 | Membrane separation method and membrane separation apparatus |
| KR101467253B1 (en) * | 2012-09-14 | 2014-12-01 | 주식회사 부강테크 | Membrane filter having fixed vortex-inducing layers |
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